CN102876371A - Inferior raw material hydrocracking method - Google Patents
Inferior raw material hydrocracking method Download PDFInfo
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- CN102876371A CN102876371A CN2011101927637A CN201110192763A CN102876371A CN 102876371 A CN102876371 A CN 102876371A CN 2011101927637 A CN2011101927637 A CN 2011101927637A CN 201110192763 A CN201110192763 A CN 201110192763A CN 102876371 A CN102876371 A CN 102876371A
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Abstract
The invention discloses an inferior raw oil hydrocracking method. According to the method, after the inferior raw oil undergoes pre-hydrofining, the raw oil and hydrogen enter a reactor in a countercurrent way; hydrofined oil enters a separator over a hydrocracking reactor at a certain linear velocity for gas-liquid separation; the upper portion of a catalyst bed is provided with several layers of cap cover trays and sieve trays, thus achieving liquid seal and mass transfer enhancement effects, avoiding hydrogen sulfide and ammonia gas from contacting with the hydrocracking catalyst and reducing the activity of the catalyst; and simultaneously, the trays have an effect of redistributing refined oil, and the refined oil uniformly enters the catalyst bed. The method provided by the invention is beneficial to performing the activity of the cracking catalyst, increasing the yield of light oil and prolonging service life of the catalyst.
Description
Technical field
The present invention relates to a kind of method for hydrogen cracking, specifically a kind of processing method that adopts one-stage serial hydrocracking processing inferior raw material.
Background technology
In recent years, along with the day by day in poor quality of the in short supply and oil property of worldwide crude resources, the character that hydroeracking unit processes raw material is day by day heaviness and in poor quality also, relative oil density, and sulphur content and nitrogen content constantly rise.At present, the nitrogen content that domestic hydroeracking unit processes raw material generally is lower than 0.2%, but the processing of high nitrogen inferior, sour feedstock has become the problem that each oil refining enterprise must be faced and need to solve.Its main solution route is the raising of catalyst performance and the optimization of processing condition etc.
Along with realizing that in recent years production process cleans, produces the development of the situations such as clean fuel, Sulfur-Containing Crude, increase yield of light oil, raising Integrated Refinery And Petrochemical productivity effect, hydrocracking technology receives increasing concern.The wide scope of material that hydrocracking can be processed, the range of product that hydrocracking is produced is many and quality is good, but common high-quality petrochemical materialss such as the clean fuel such as direct production liquefied gas, gasoline, kerosene, rocket engine fuel, diesel oil and light naphthar, heavy naphtha, tail oil.And hydrocracking technology also has production decision flexibly and the liquid product yield high.
Existing hydrocracking process technology is stock oil and hydrogen and flow to into hydrofining reactor normally, by beds carry out the hydrogenation saturation of olefins, take off virtue, denitrogenation and deoxidation etc.Directly enter hydrocracking reactor from hydrofining reactor gas-liquid mixture out, carry out open loop and macromole cracking, lighting at beds.From hydrocracking reactor gas-liquid mixture out, isolate gas and water after, generate oil through fractionation plant, fractionation obtains various distillates.The method is applicable to nitrogen and the lower stock oil of oxygen level.And for nitrogen content and the higher raw material of oxygen level, in unifining process, will produce a large amount of ammonia and water, and these materials and treated oil together enter cracking case, and ammonia is easy to and the combination of acidity of catalyst center, causes the catalyzer cracking activity to reduce; In addition, the water vapour of reaction process generation is also influential to the performance of catalyzer.
US2003085154 discloses a kind of method for hydrogen cracking of processing the high nitrogen-containing distillate.Establish flash tank with cutting out partial foreign gas between two hydrofining reactors of the method employing and hydrocracking reactor serial operation, hydrofining reactor.The method adopts the parallel feeding mode, namely circulate tail oil with enter successively the first hydrofining reactor, flash tank, the second hydrofining reactor and hydrocracking reactor after fresh feed mixes, so the hydrogen consumption is large, circulating hydrogen compressor is loaded greatly.In addition, because the method refining stage reaction product directly enters hydrocracking reactor, so product selectivity is poor, and the middle runnings yield is low.
CN1045462C discloses the method for hydrogen cracking that a kind of heavy raw oil is produced diesel oil.The method is hydrofining reactor and hydrocracking reactor serial operation, and is middle without separating device.The method stock oil bad adaptability, diesel yield is low.
Summary of the invention
Deficiency for existing complete processing the invention provides a kind of improved one-stage serial hydrocracking processing method, and inferior feedstock oil with the reverse reactor that enters of hydrogen, can increase the yield of light-weight fuel oil after hydrofining, improve the quality of products.Wherein, hydrofined oil enters the disengaging zone of hydrocracking reactor top, carry out gas-liquid separation, beds top is provided with some layers column plate, play the effect of fluid-tight and reinforcing mass transfer, avoid hydrogen sulfide, ammonia and hydrocracking catalyst to contact, reduce the activity of catalyzer, column plate has the effect of reallocation to treated oil simultaneously, makes treated oil enter uniformly beds.
Inferior raw material method for hydrogen cracking of the present invention comprises following content:
(1) inferior feedstock oil with enter hydrofining reactor after hydrogen mixes and carry out hydrofining reaction;
(2) the hydrofining reaction resultant enters the separator of cracking case top, carries out gas-liquid separation, then separates with the enterprising stepping promoting the circulation of qi liquid of column plate that the hydrogen that makes progress arranges on reactor top, and carries out the distribution of mass transfer and treated oil;
(3) treated oil and the reverse hydrocracking catalyst bed that passes through of hydrogen that are evenly distributed through column plate carry out hydrocracking reaction;
(4) step (3) gained hydrocracking generates oil and enter separation column after separating, and obtains light-end products (generally comprising gas, petroleum naphtha, kerosene and diesel oil) and hydrogenation tail oil through fractionation.
According to inferior raw material working method of the present invention, wherein doing of the inferior raw material described in the step (1) is generally 540 ~ 590 ℃, and nitrogen content generally more than 0.2wt%, is generally 0.2 ~ 1.5 wt%.Sulphur content generally more than 1wt%, is generally more than the 1.5wt%.Described inferior raw material generally is selected from the various coker gas oils (CGO) that obtain of processing middle-eastern crude, such as among Iranian CGO, the Saudi Arabia CGO etc. one or several; Also can be the shale oil full distillate oil that the processing oil shale retorting is produced, such as a thousand pieces of gold shale oil of Fushun Mining Group, in the near coal-mine shale oil one or several.
Step (1) adopts conventional hydrofining technology, and described hydrofining reaction operational condition is: reaction pressure is 3.0MPa～19.0 MPa, is preferably 4.0MPa～16.0 MPa; Average reaction temperature is 280 ℃～460 ℃, is preferably 300 ℃～420 ℃; Volume space velocity 0.1～6.0 h
-1, be preferably 0.3～4.0 h
-1Hydrogen to oil volume ratio 300: 1～3000: 1 is preferably 500: 1～2500: 1.
Column plate described in the step (2) is positioned at the below of separator, the top of beds.1～10 layer of calotte column plate can be installed separately, also can arrange in pairs or groups 1～6 layer of calotte column plate and 1～5 layer of sieve tray are installed.Described calotte column plate and sieve tray play the effect of treated oil reallocation, fluid-tight, further gas-liquid separation and mass transfer, and wherein the column plate number of plies is preferably 2～3 layers of calotte column plate and 1～2 layer of sieve tray.
The operational condition of the described hydrocracking reaction of step (3) is: reaction pressure is 3.0MPa～19.0 MPa, is preferably 4.0MPa～18.0 MPa; Average reaction temperature is 290 ℃～460 ℃, is preferably 320 ℃～440 ℃; Volume space velocity 0.1～5.0 h
-1, be preferably 0.3～4.0 h
-1Hydrogen to oil volume ratio 300: 1～3000: 1 is preferably 500: 1～2500: 1.
In the step (4), reacted hydrogen-rich gas is discharged from the top of hydrocracking reactor, enters cold high pressure separator after injecting washing water, separates the liquid hydrocarbon streams that obtains, and can generate with cracking further to process after oil mixes.The water injection rate of washing water is the 5wt%～20wt% of device general design oil inlet quantity, and preferred water injection rate is the 12wt%～18wt% of design oil inlet quantity.The waste water that contains in a large number ammonium salt that washing obtains drains into waste disposal plant outward.Described cold high pressure separator working pressure and reacting system pressure are basic identical, and temperature is generally 10～90 ℃, preferred 35～65 ℃.
Compared with prior art, method of the present invention has the following advantages:
1, hydrofined oil and hydrogen adverse current are by hydrocracking reactor, and the gas phase that cracking reaction generates and treated oil generate gas and together discharge from reactor top, and hydrogen recycle is used after washing separates; Hydrocracking generates oil and discharges from reactor bottom, enters separation column.Flow process of the present invention has been saved the higher thermal high tripping device of cost in the conventional hydrocracking process process.
2, the separator of cracking case top setting can make generation oil and the gas delivery in the refining reaction effluent; Treated oil after the separation carries out mass transfer with hydrogen from bottom to top at column plate, and further realizes gas-liquid separation.
3, owing to there being certain height of liquid layer treated oil to exist on the calotte column plate that the separator bottom arranges and the sieve tray, play " fluid-tight " effect, make ammonia and water vapour in the hydrotreated product can not enter the hydrocracking catalyst bed, can performance and the acid sites of cracking catalyst do not exerted an influence.Be conducive to the performance of cracking catalyst activity, increase the yield of light-end products, the work-ing life of extending catalyst.
4, the column plate, particularly sieve tray of the setting of cracking case top are reallocated to the treated oil that enters reactor, make the treated oil state of being evenly distributed enter beds.Be conducive to taking full advantage of of catalyst activity, effectively avoided channel and local reaction too violent.
5, refining generation oil is downward along the cracking catalyst bed, with the hydrogen contact reacts that makes progress, because density of hydrogen increases to the bottom gradually from beds top, the carrying out that is conducive to hydrogenation reaction, also can reduce simultaneously the hydrogen-oil ratio of hydrocracking reaction, be conducive to the smooth operation of hydrocracking reactor.
Description of drawings
Fig. 1 is the schematic flow sheet of inferior raw material method for hydrogen cracking of the present invention.
Embodiment
In the method for hydrogen cracking of the present invention, wherein the described Hydrobon catalyst of step (1) can be the Hydrobon catalyst of routine, and catalyzer comprises the hydrogenation active metals of carrier and institute's load.Take the weight of catalyzer as benchmark, generally include metal component of group VIB in the periodic table of elements, count 10wt%～35wt% such as tungsten and/or molybdenum with oxide compound, be preferably 15wt%～30wt%; Group VIII metal such as nickel and/or cobalt are counted 1wt %～7wt% with oxide compound, are preferably 1.5wt%～6wt%.Carrier is inorganic refractory oxide, generally is selected from aluminum oxide, amorphous silicon aluminium, silicon-dioxide, titanium oxide etc.Can select existing various commercial catalysts, such as FF-14, FF-24,3936,3996, FF-16, FF-26, the Hydrobon catalysts such as FF-36, FF-46 of Fushun Petrochemical Research Institute (FRIPP) development; HC-K, HC-P that Uop Inc. produces; TK-555, TK-565 catalyzer that Topsoe company produces also can be as required be prepared by the general knowledge of this area.
The described hydrocracking catalyst of step (3) comprises cracking component and hydrogenation component.The cracking component generally includes amorphous aluminum silicide and/or molecular sieve, such as Y type or USY molecular sieve.Tackiness agent is generally aluminum oxide or silicon oxide.Hydrogenation component is selected from metal, metal oxide or the metallic sulfide of VI family, VII family or VIII family, more preferably one or more in iron, chromium, molybdenum, tungsten, cobalt, nickel or its sulfide or the oxide compound.Take the weight of catalyzer as benchmark, the content of hydrogenation component is 5～40wt%.Conventional hydrocracking catalyst can be selected existing various commercial catalysts, FC-12, the FC-14 that develops such as FRIPP, FC-16, FC-24, FC-26, ZHC-02, FC-28 etc.; The catalyzer such as the HC-12 of Uop Inc., HC-14, HC-24, HC-39 also can be as required prepare specific hydrocracking catalyst by the general knowledge of this area.
Below in conjunction with accompanying drawing method of the present invention is elaborated.
As shown in Figure 1, hydrocracking process flow process of the present invention is as follows:
Next by specific embodiment inferior raw material hydrocracking method of the present invention is further described.That use in embodiment and the comparative example is conventional hydrofining agent FF-36 and the hydrocracking catalyst FC-14 of Fushun Petrochemical Research Institute's development and production.Its character sees Table 1.Stock oil character sees Table 2.
The main physico-chemical property of table 1 catalyzer
| Project | FF-36 | FC-14 |
| Physical properties | The trifolium bar | Cylindrical bars |
| Particle diameter, mm | 1.1~1.3 | 1.5~1.7 |
| Bar is long, |
3~8 | 3~8 |
| Chemical constitution, wt%: | ? | ? |
| NiO | 3.9 | 5.3 |
| MoO 3 | 23.6 | — |
| WO 3 | — | 22.1 |
Table 2 stock oil character
| Project | Stock oil |
| Density (20 ℃)/gcm -3 | 0.9105 |
| Boiling range/℃ (GB/T 9168-1997) | 250～580 |
| Sulphur/wt% | 1.22 |
| Nitrogen/mgg -1 | 2900 |
Hydrobon catalyst is FF-36, and hydrocracking catalyst is FC-14, and the inventive method is adopted in technical process, and the raw material oil properties sees Table 2, reaction conditions and the results are shown in Table 3.
Comparative example 1
Hydrobon catalyst is FF-36, and hydrocracking catalyst is FC-14, and the common process flow process is adopted in technical process, and the hydrofining reaction effluent enters the hydrocracking reactor top, and the operating method that adopts gas and liquid flowing to flow downward is carried out the hydrocracking operation.
Table 3 embodiment 1 and comparative example 1 data
| ? | |
Comparative example 1 |
| Catalyzer | FF-36 /FC-14 | FF-36 /FC-14 |
| Reaction pressure/ |
12 | 12 |
| Average reaction temperature/℃ | 360/365 | 360/365 |
| Volume space velocity/h -1 | 0.6/0.6 | 0.6/0.6 |
| Hydrogen to oil volume ratio, v/v | 1000/600 | 1000/1200 |
| Refining nitrogen in the oil, the mgg of generating -1 | 105 | 106 |
| Refining sulphur in the oil, the mgg of generating -1 | 32 | 37 |
| ＜177 ℃ of cut yields, wt% | 3.97 | 2.41 |
| 177 ~ 350 ℃ of cut yields, wt% | 67.82 | 54.37 |
Hydrobon catalyst is FF-36, and hydrocracking catalyst is FC-14, and the inventive method is adopted in technical process, and the raw material oil properties sees Table 2, reaction conditions and the results are shown in Table 4.
Comparative example 2
Hydrobon catalyst is FF-36, and hydrocracking catalyst is FC-14, and the common process flow process is adopted in technical process, and the hydrofining reaction effluent enters the hydrocracking reactor top, and the operating method that adopts gas and liquid flowing to flow downward is carried out the hydrocracking operation.
Table 4 embodiment 2 and comparative example 2 data
| ? | |
Comparative example 2 |
| Catalyzer | FF-36 /FC-14 | FF-36 /FC-14 |
| Reaction pressure/ |
14 | 14 |
| Average reaction temperature/℃ | 365/362 | 365/362 |
| LHSV/h -1 | 0.5 | 0.5 |
| Hydrogen to oil volume ratio, v/v | 800/500 | 800/1000 |
| Refining nitrogen in the oil, the mgg of generating -1 | 93 | 92 |
| Refining sulphur in the oil, the mgg of generating -1 | 26 | 24 |
| ＜177 ℃ of cut yields, wt% | 4.97 | 3.75 |
| 177 ~ 350 ℃ of cut yields, wt% | 70.36 | 59.61 |
Claims (10)
1. inferior raw material method for hydrogen cracking may further comprise the steps:
(1) inferior feedstock oil with enter hydrofining reactor after hydrogen mixes and carry out hydrofining reaction;
(2) the hydrofining reaction resultant enters the separator of cracking case top, carries out gas-liquid separation, then separates with the enterprising stepping promoting the circulation of qi liquid of column plate that the hydrogen that makes progress arranges on reactor top, and carries out the distribution of mass transfer and treated oil;
(3) treated oil and the reverse hydrocracking catalyst bed that passes through of hydrogen that are evenly distributed through column plate carry out hydrocracking reaction;
(4) step (3) gained hydrocracking generates oil and enter separation column after separating, and obtains light-end products and hydrogenation tail oil through fractionation.
2. according to method for hydrogen cracking claimed in claim 1, it is characterized in that, doing of described inferior raw material is 540 ~ 590 ℃, and nitrogen content is more than 0.2wt%, and sulphur content is more than 1wt%.
3. according to method for hydrogen cracking claimed in claim 1, it is characterized in that, described column plate comprises 1～10 layer of calotte column plate, perhaps comprises 1～6 layer of calotte column plate and 1～5 layer of sieve tray.
4. according to method for hydrogen cracking claimed in claim 1, it is characterized in that, described hydrofining reaction operational condition is: reaction pressure is 3.0MPa～19.0 MPa, and average reaction temperature is 280 ℃～460 ℃, volume space velocity 0.1～6.0 h
-1, hydrogen to oil volume ratio 300: 1～3000: 1.
5. according to method for hydrogen cracking claimed in claim 1, it is characterized in that, the operational condition of the described hydrocracking reaction of step (3) is: reaction pressure is 3.0MPa～19.0 MPa, and average reaction temperature is 290 ℃～460 ℃, volume space velocity 0.1～5.0 h
-1, hydrogen to oil volume ratio 300: 1～3000: 1.
6. according to method for hydrogen cracking claimed in claim 1, it is characterized in that, isolated hydrogen-rich gas is discharged from the top of hydrocracking reactor in the step (2), enters cold high pressure separator after injecting washing water.
7. according to method for hydrogen cracking claimed in claim 6, it is characterized in that, the water injection rate of described washing water is the 5wt%～20wt% of device general design oil inlet quantity.
8. according to method for hydrogen cracking claimed in claim 1, it is characterized in that, described light-end products comprises petroleum naphtha, kerosene and diesel oil.
9. according to method for hydrogen cracking claimed in claim 1, it is characterized in that, described Hydrobon catalyst comprises carrier and hydrogenation active metals, take catalyst weight as benchmark, comprise that the group VIB metal counts 10wt%～35wt% with oxide compound, group VIII metal is counted 1wt%～7wt% with oxide compound.
10. according to method for hydrogen cracking claimed in claim 1, it is characterized in that, described hydrocracking catalyst comprises cracking component and hydrogenation component, and take the weight of catalyzer as benchmark, the content of hydrogenation component is counted 5wt%～40wt% with oxide compound.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN109988609A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of flexible hydrogenation of shale oil process |
| CN115785995A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Inferior diesel oil hydrotreating method and device |
| CN115785993A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Diesel hydrogenation method and device |
| CN115785994A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Wax oil hydrogenation method and device |
| CN115785992A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Startup method of inferior diesel hydrogenation process |
| CN116064122A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | Method and device for producing aromatic hydrocarbon raw material by coal tar hydrogenation treatment |
| CN116064131A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | Fischer-Tropsch synthesis oil hydrotreatment device and method |
| CN115785993B (en) * | 2021-09-10 | 2024-05-31 | 中国石油化工股份有限公司 | Diesel hydrogenation method and device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1205318C (en) * | 2002-10-10 | 2005-06-08 | 中国石油化工股份有限公司 | Poor residuum hydroconversion method |
| CN101942333A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Shale oil single-stage serial hydrocracking technology method |
-
2011
- 2011-07-11 CN CN201110192763.7A patent/CN102876371B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1205318C (en) * | 2002-10-10 | 2005-06-08 | 中国石油化工股份有限公司 | Poor residuum hydroconversion method |
| CN101942333A (en) * | 2009-07-09 | 2011-01-12 | 中国石油化工股份有限公司抚顺石油化工研究院 | Shale oil single-stage serial hydrocracking technology method |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109988609A (en) * | 2017-12-29 | 2019-07-09 | 中国石油化工股份有限公司 | A kind of flexible hydrogenation of shale oil process |
| CN109988609B (en) * | 2017-12-29 | 2021-05-04 | 中国石油化工股份有限公司 | Flexible shale oil hydrocracking process |
| CN115785995A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Inferior diesel oil hydrotreating method and device |
| CN115785993A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Diesel hydrogenation method and device |
| CN115785994A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Wax oil hydrogenation method and device |
| CN115785992A (en) * | 2021-09-10 | 2023-03-14 | 中国石油化工股份有限公司 | Startup method of inferior diesel hydrogenation process |
| CN115785993B (en) * | 2021-09-10 | 2024-05-31 | 中国石油化工股份有限公司 | Diesel hydrogenation method and device |
| CN116064122A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | Method and device for producing aromatic hydrocarbon raw material by coal tar hydrogenation treatment |
| CN116064131A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | Fischer-Tropsch synthesis oil hydrotreatment device and method |
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